EP1831263B1 - Appareil et procédé pour la polymérisation d'oléfines en phase gazeuse - Google Patents

Appareil et procédé pour la polymérisation d'oléfines en phase gazeuse Download PDF

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Publication number
EP1831263B1
EP1831263B1 EP05814363A EP05814363A EP1831263B1 EP 1831263 B1 EP1831263 B1 EP 1831263B1 EP 05814363 A EP05814363 A EP 05814363A EP 05814363 A EP05814363 A EP 05814363A EP 1831263 B1 EP1831263 B1 EP 1831263B1
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European Patent Office
Prior art keywords
gas
filter
filter medium
reactor
inlet chamber
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EP05814363A
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German (de)
English (en)
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EP1831263A1 (fr
Inventor
Eberhard Herrmann
Manfred Hecker
Rainer Karer
Klaus Berhalter
Paulus De Lange
Jörg HALPAP
Cyrus Ahmadzade-Youssefi
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Basell Polyolefine GmbH
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Basell Polyolefine GmbH
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/0015—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor
    • B01J8/003—Feeding of the particles in the reactor; Evacuation of the particles out of the reactor in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/005—Separating solid material from the gas/liquid stream
    • B01J8/006—Separating solid material from the gas/liquid stream by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/18—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with fluidised particles
    • B01J8/1872—Details of the fluidised bed reactor
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F10/00—Homopolymers and copolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00168—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles
    • B01J2208/00256—Controlling the temperature by indirect heat exchange with heat exchange elements outside the bed of solid particles in a heat exchanger for the heat exchange medium separate from the reactor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00008—Controlling the process
    • B01J2208/00017—Controlling the temperature
    • B01J2208/00106—Controlling the temperature by indirect heat exchange
    • B01J2208/00265—Part of all of the reactants being heated or cooled outside the reactor while recycling
    • B01J2208/00274—Part of all of the reactants being heated or cooled outside the reactor while recycling involving reactant vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00743—Feeding or discharging of solids
    • B01J2208/00761—Discharging
    • C—CHEMISTRY; METALLURGY
    • C08—ORGANIC MACROMOLECULAR COMPOUNDS; THEIR PREPARATION OR CHEMICAL WORKING-UP; COMPOSITIONS BASED THEREON
    • C08F—MACROMOLECULAR COMPOUNDS OBTAINED BY REACTIONS ONLY INVOLVING CARBON-TO-CARBON UNSATURATED BONDS
    • C08F110/00—Homopolymers of unsaturated aliphatic hydrocarbons having only one carbon-to-carbon double bond
    • C08F110/02—Ethene

Definitions

  • the present invention relates to an apparatus for the polymerization of olefins, in particular ethylene, comprising a gas-phase fluidized-bed reactor, a product offtake line for taking polymer particles either continuously or discontinuously from the reactor, which line is connected to a depressurization vessel for separating polymer particles and gas, a recycle gas filter for freeing the gas of entrained fine particles connected to the depressurization vessel, a compressor which compresses the gas which has been freed of fine particles and recirculates it into the reactor, with the recycle gas filter having an inlet chamber provided with a gas inlet, an outlet chamber provided with a gas outlet, an essentially vertical sheet-like filter medium for retaining the fine particles which separates the inlet chamber from the outlet chamber and a particle outlet.
  • Gas-phase polymerization processes are economical processes for the polymerization of ethene and propene or for the copolymerization of ethene or propene with other C 2 -C 8 - ⁇ -olefins.
  • Such gas-phase polymerization processes can be configured, in particular, as gas-phase fluidized-bed processes in which the polymer particles are kept in suspension by means of a suitable gas stream. Processes of this type are described, for example, in EP-A-0 475 603 , EP-A-0 089 691 and EP-A-0 571 826 , whose contents are hereby fully incorporated by reference.
  • the polymer particles present in the fluidized bed are discharged continuously or discontinuously and conveyed pneumatically into a depressurization vessel.
  • considerable amounts of gas are also discharged from the reactor and it is sensible to recirculate this gas to the process.
  • the gas which has been separated off from the polymer particles in the depressurization vessel and still contains considerable amounts of fine dust cannot be returned directly to the reactor circuit but instead firstly has to be substantially freed of the fine particles in order to avoid deposits in the compressor.
  • Recycled gas filters comprising batteries of bag filters are usually employed for this purpose, since such filters have a relatively long period of operation even at high dust loadings.
  • DE 39 30 765 C1 discloses a bag filter in which an upper wall section and a lower wall section are used in the inlet region of the filter to make transverse and longitudinal flow onto the filter possible and make the dust deposition over the filter area more uniform.
  • the upper wall section and the lower wall section are mounted so as to allow them to be swiveled horizontally relative to one another so as to be able to influence the ratio of the flow from below to the flow from the side.
  • the flow from the side is brought about by means of a fixed dividing wall for the gas.
  • Such an arrangement is firstly quite complicated and secondly the stability of the filter cake leaves something to be desired.
  • the inlet chamber having a dividing wall which is arranged essentially parallel to the filter medium and divides the inlet chamber into an inflow region which is connected to the gas inlet and a filter region in which the filter medium is located and has an upper opening and a lower opening which are dimensioned so that from 60 to 90% of the volume flow flows through the upper opening so that flow along the filter medium from the top downward results.
  • An important aspect of the solution provided according to the invention is that the proportion of the gas to be purified flowing onto the filter medium from above is significantly higher than the proportion flowing onto the filter medium from below. In this way, a high gas throughput (high volume flow) through the filter is achieved at a relatively low flow velocity along the filter.
  • the formation of a filter cake which can readily be cleaned off is aided by the cleaning of the filter being achieved both by means of gravity and by means of the gas flowing onto the filter from the top downward.
  • the arrangement according to the invention might prevent fine particles which have been cleaned off redepositing on the filter and forming a filter cake which can no longer be cleaned off completely (unstable filter cake), without being bound to this explanation.
  • the filter is therefore particularly suitable for polymerization plants using a fluidized-bed reactor, since large amounts of fine dust are frequently formed here, without being restricted to this application.
  • the filter of the invention is in principle suitable for all applications in which the formation of an unstable filter cake due to high proportions of fines is to be prevented.
  • the inlet chamber is divided into two regions, viz. an inflow region and a filter region.
  • the inflowing particle-containing gas does not impinge directly on the filter but is instead distributed over the filter area via the upper and lower openings in the dividing wall. Erosion of the filter material in long-term operation is avoided thereby.
  • the risk of tearing the filter material is considerably reduced by appropriate dimensioning of the upper and lower openings, even in the case of pressure surges which occur in particular during discontinuous removal of the polymer product from the polymerization reactor.
  • filters it is possible to use all filter types which operate using sheet-like filter media. They can also be surface or deep-bed filters, with surface filters being preferred. Bag filters, preferably in the form of batteries of bag filters, are most frequently used. However, envelope filters or cartridge filters can also be used. All customary filter media are in principle suitable as filter media. The only restriction in terms of the material is in respect of its fire resistance so that the filter medium does not ignite when the filter is opened in the presence of metal alkyls. Preference is given to using nonwovens or woven fabrics, for example materials of this type made of glass, metal or preferably noncombustible plastics such as polyphenylene sulfide (PPS). Information on the selection and design of the filter media may be found, for example, in Ullmann's Encyclopedia of Industrial Chemistry, 6th Edition, 2000 Electronic Release, whose contents are hereby fully incorporated by reference.
  • PPS polyphenylene sulfide
  • the filter efficiency after a stable filter cake has been built up is usually above 99%, preferably above 99.9%.
  • the flow can be reversed briefly at regular intervals, with such cleaning being carried out at short intervals by means of the arrangement according to the invention. According to the invention, such cleaning at regular intervals is preferred.
  • the dividing wall is cylindrical and the filter medium is located in the interior of the cylinder.
  • bag filters arranged in parallel are preferred.
  • the upper and lower openings of the dividing wall can in this way be configured as annular gaps which allow very uniform flow onto the filter.
  • the inlet chamber is cylindrical and the gas inlet is connected eccentrically, in particular essentially tangentially, to the inlet chamber. Preliminary deposition of the filter dust in the inflow region is achieved in this way.
  • the inlet chamber and the dividing wall being cylindrical and the central axes being essentially vertical.
  • the cylindrical dividing wall completely surrounds the filter material in such a case.
  • the design of the upper and lower openings to distribute the volume flows can be calculated by engineering methods or determined by simple experiments.
  • the throughput per unit area through the filter should usually not exceed 120 m 3 /m 2 h, with a throughput per unit area through the filter of from 20 to 100 m 3 /m 2 h being preferred and a throughput per unit area through the filter of from 30 to 60 m 3 /m 2 h being particularly preferred.
  • the present invention further provides a process for the polymerization of olefins, in which the olefin is polymerized in the presence of a catalyst in a gas-phase fluidized-bed reactor, the polymer particles are taken off continuously or discontinuously from the reactor, the polymer particles are separated from the gas carried out together with them and the gas is freed of entrained fine particles by means of a recycle gas filter, compressed and at least partly recirculated to the reactor, with the recycle gas filter having an essentially vertical sheet-like filter medium for retaining the fine particles, wherein from 60 to 90% of the volume flow flows onto the filter medium from above, so that a flow along the filter medium from the top downward results.
  • Figure 1 shows the construction of a polymerization plant having a gas-phase fluidized-bed reactor.
  • a gas-phase fluidized bed usually consists of particles which are kept suspended in the gas phase by a stream of gas.
  • the fluidized bed can comprise not only a gas or gas mixture but also condensed material as fluid.
  • the actual reactor 1 comprises a cylindrical tube.
  • the fluidized bed 1b is usually bounded at the bottom by a gas distributor plate 1 a.
  • a widening calming zone 1c which reduces the discharge of particles from the reactor 1.
  • the calming zone can be omitted.
  • the reaction gas leaves the reactor 1 at the upper end of the calming zone and is conveyed in the gas circulation line via a cyclone 12 to the compressor 14 and from there via a heat exchanger 13 in which the recycle gas is cooled back to the reactor 1.
  • the circulated reactor gas is usually a mixture of ethene or propene, if desired a molecular weight regulator such as hydrogen and inert gases such as nitrogen and/or saturated hydrocarbons such as ethane, propane, butane, pentane or hexane.
  • the reactor gas can further comprise C 3 -C 8 - ⁇ -olefins such as propene, 1-butene, 1-pentene, 2-methylpentene, 1-hexene, 1-heptene and 1-octene, which may also be present in condensed form, as comonomers.
  • the velocity of the reactor gas has to be sufficient firstly to fluidize the mixed loose bed of finely divided polymer which is present in the tube and serves as polymerization zone and secondly to remove the heat of polymerization effectively.
  • the constituents of the reactor gas can be fed directly into the gas-phase fluidized-bed reactor or into the circulated reactor gas.
  • the capacity of the gas-phase fluidized-bed reactor is, as is known, limited by the cooling capacity of the circulated reactor gas.
  • This cooling capacity depends firstly on the pressure under which the reactor gas is maintained or at which the (co)polymerization is carried out. It is generally advisable to work at pressures of from 0.1 to 10 MPa, preferably from 1 to 8 MPa and in particular from 1.5 to 5 MPa. In addition, the cooling capacity depends on the temperature at which the (co)polymerization is carried out in the fluidized bed.
  • temperatures in the process of the invention it is advantageous to work at temperatures of from 30 to 125°C, particularly preferably from 75 to 118°C, with temperatures in the upper part of this range preferably being set for copolymers having a relatively high density and temperatures in the lower part of this range preferably being set for copolymers having a relatively low density. Furthermore, the amount of catalyst metered in determines the product output.
  • the proportion of inert gases such as nitrogen or inert hydrocarbons has an influence on the risk of conglutinations and deposits occurring.
  • High proportions of inert gas can reduce the risk of deposits, but can at the same time adversely affect the space-time yield as a result of low catalyst productivities, so that the process can become uneconomical.
  • the proportion of inert gas is preferably from 15 to 75% by volume, particularly preferably from 35 to 50% by volume, based on the total volume of the reaction gas.
  • catalysts it is possible to use all known types of catalyst which are suitable for olefin polymerization. Particular mention may be made of Ziegler catalysts, chromium-based Phillips catalysts and single-site catalysts, in particular metallocene catalysts, without being restricted thereto.
  • the polymer is discharged continuously or discontinuously through one or more discharge lines 15.
  • the polymer is freed of the major part of the gas discharged with it in a depressurization vessel 2 and is passed to the further processing units.
  • the gas which has been separated from the polymer and which contains considerable amounts of entrained fine dust is fed into the recycle gas filter 3 in which the gas is largely freed of the fine dust.
  • the purified gas is compressed to the reactor pressure in a compressor 11 and fed into the circulating gas.
  • Figure 2 schematically shows a vertical section through a recycle gas filter 3 according to the invention, and figure 3 shows a horizontal section through such a filter 3.
  • the recycle gas filter is essentially cylindrical and contains an inlet or raw gas region 4 in its lower region and an outlet or clean gas region 5 in its upper region. Inlet region and outlet region are separated by the sheet-like filter medium 9.
  • the filter medium is installed in the form of bag filter batteries 9 which extend vertically in the recycle gas filter 3.
  • the inlet gas region 4 extends downward in the shape of a truncated cone and finally ends in a particle outlet 8 via which the retained particles from the recycle gas filter 3 can be discharged.
  • the fine dust is discontinuously returned to the depressurization vessel 2 and added to the polymer.
  • the inlet region 4 is divided by a dividing wall 10 into two regions, viz. an inflow region 4a and a filter region 4b.
  • the dividing wall 10 likewise extends in the form of a cylinder into the inlet region 4, so that the inflow region 4a has a circular cross section.
  • the dividing wall has an upper opening and a lower opening in the form of annular gaps, with the ratio of the gap widths of the upper gap and the lower gap being about 1.9, so that the proportion of the volume flow which flows through the upper annular gap is about 65%.
  • the gaps are dimensioned so that the gas flowing through the gas inlet is distributed sufficiently over the bag filters without a significant pressure drop being produced.
  • the gaps prefferably be fixed or else for the cylindrical dividing wall 10 to be mounted so that it can be moved vertically in order to alter the flow coming in from the top and from below during operation and thus adapt the operating conditions.
  • the flow direction of the raw gas is indicated by arrows.
  • the bag filters 9 are conventional commercially available bag filters comprising noncombustible filter material, for example polyphenylene sulfide (PPS).
  • PPS polyphenylene sulfide
  • the filters are cleaned at regular intervals by reversal of the flow.
  • the use of such cleaning is generally known to those skilled in the art and is described, for example, in Ullmann's Encyclopedia of Industrial Chemistry, 6th Edition, 2000 Electronic Release.
  • the dividing wall (10) is held in place by struts which are welded to the cylindrical vessel.
  • the excellent operating time behavior of the recycle gas filter of the invention is made particularly clear by a polymerization plant comprising a gas-phase fluidized-bed reactor having a product output of about 250 000 metric tons per annum not requiring replacement of the filter elements over a period of about 2.5 years

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Health & Medical Sciences (AREA)
  • Medicinal Chemistry (AREA)
  • Polymers & Plastics (AREA)
  • Engineering & Computer Science (AREA)
  • Combustion & Propulsion (AREA)
  • Polymerisation Methods In General (AREA)

Abstract

L'invention concerne un appareil pour la polymérisation d'oléfines, en particulier de l'éthylène, comprenant un réacteur à lit fluidisé en phase gazeuse (1), une ligne de soutirage de produit (15) servant à soutirer des particules de polymère soit en continu soit de façon discontinue du réacteur (1), laquelle ligne (15) est reliée à une cuve de dépressurisation (2) servant à séparer les particules de polymère et le gaz, un filtre pour le gaz recyclé (3) servant à éliminer du gaz les fines particules entraînées et relié à la cuve de dépressurisation (2), un compresseur qui comprime le gaz dont on a enlevé les fines particules et qui le fait recirculer vers le réacteur (1), le filtre pour le gaz recyclé (3) ayant une chambre d'entrée (4) pourvue d'une entrée pour le gaz (6), une chambre de sortie (5) pourvue d'une sortie pour le gaz (7), un milieu de filtration pratiquement vertical ressemblant à une feuille (9) servant à retenir les fines particules qui sépare la chambre d'entrée (4) de la chambre de sortie (5) et une sortie pour les particules (8). La chambre d'entrée (4) a une paroi de séparation (10) qui est disposée de façon pratiquement parallèle au milieu de filtration (9) et qui sépare la chambre d'entrée (4) en une zone de flux entrant (4a) qui est reliée à l'entrée pour le gaz (6) et une zone de filtration (4b) dans laquelle est situé le milieu de filtration et qui a une ouverture supérieure et une ouverture inférieure qui sont dimensionnées de façon à ce que de 60 à 90 % du flux en volume passe par l'ouverture supérieure de façon à ce qu'il en résulte un écoulement le long du milieu de filtration (9) allant du haut vers le bas.

Claims (8)

  1. Appareil pour la polymérisation d'oléfines, en particulier de l'éthylène, qui comprend un réacteur à lit fluidisé en phase gazeuse (1), une ligne de soutirage de produit (15) pour soutirer de façon continue ou discontinue les particules de polymère du réacteur (1), laquelle ligne (15) est reliée à une cuve de dépressurisation (2) pour séparer les particules de polymère et le gaz, un filtre pour le gaz recyclé (3) pour éliminer du gaz les fines particules entraînées, lequel filtre est relié à la cuve de dépressurisation (2), un compresseur qui comprime le gaz dont on a enlevé les fines particules et qui le fait recirculer vers le réacteur (1), le filtre pour le gaz recyclé (3) comprenant une chambre d'entrée (4) pourvue d'une entrée pour le gaz (6), une chambre de sortie (5) pourvue d'une sortie pour le gaz (7), un milieu de filtration essentiellement vertical en forme d'une feuille (9) pour retenir les fines particules qui sépare la chambre d'entrée (4) de la chambre de sortie (5), ainsi qu'une sortie pour les particules (8), dans lequel la chambre d'entrée (4) possède une paroi de séparation (10) qui est disposée de façon essentiellement parallèle au milieu de filtration (9) et qui sépare la chambre d'entrée (4) en une zone de flux entrant (4a) laquelle est reliée à l'entrée pour le gaz (6), et une zone de filtration (4b) dans laquelle est situé le milieu de filtration et qui possède une ouverture supérieure et une ouverture inférieure qui sont dimensionnées de façon à ce que de 60 à 90 % du débit en volume passe par l'ouverture supérieure de façon à ce qu'il en résulte un écoulement le long du milieu de filtration (9) allant du haut vers le bas.
  2. Appareil selon la revendication 1, dans lequel de 60 à 85 %, en particulier de 65 à 80 %, du débit en volume s'écoule par l'ouverture supérieure.
  3. Appareil selon l'une quelconque des revendications précédentes, dans lequel la paroi de séparation (10) est cylindrique et le milieu de filtration (9) est placé à l'intérieur de la paroi de séparation cylindrique (10).
  4. Appareil selon l'une quelconque des revendications précédentes, dans lequel la chambre d'entrée (4) est cylindrique et l'entrée pour le gaz (6) est reliée de façon excentrique, en particulier essentiellement de façon tangentielle, à la chambre d'entrée (4).
  5. Appareil selon l'une quelconque des revendications précédentes, dans lequel le débit par unité de surface au travers du filtre varie de 20 à 100 m3/m2h, de préférence de 30 à 60 m3/m2h.
  6. Procédé de polymérisation d'oléfines, dans lequel l'oléfine est polymérisée en présence d'un catalyseur dans un réacteur à lit fluidisé en phase gazeuse (1), les particules de polymère sont retirées du réacteur (1) de façon continue ou discontinue, les particules de polymère sont séparées du gaz extrait avec elles et le gaz est libéré des fines particules entraînées au moyen d'un filtre pour le gaz recyclé (3), compressé et au moins partiellement recirculé vers le réacteur (1), avec le filtre pour le gaz recyclé (3) possédant un milieu de filtration essentiellement vertical en forme d'une feuille (9) pour retenir les fines particules, dans lequel de 60 à 90 % du débit en volume s'écoule sur le milieu filtrant (9) par le haut, de façon à ce qu'il en résulte un écoulement le long du milieu de filtration (9) du haut vers le bas.
  7. Procédé selon la revendication 6, dans lequel la vitesse dans l'espace intermédiaire est inférieure à 1 m/s.
  8. Procédé selon l'une quelconque des revendications 6 et 7, dans lequel le débit dans la chambre d'entrée (4a) est essentiellement tangentiel.
EP05814363A 2004-11-09 2005-11-08 Appareil et procédé pour la polymérisation d'oléfines en phase gazeuse Active EP1831263B1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102004054304A DE102004054304A1 (de) 2004-11-09 2004-11-09 Vorrichtung und Verfahren zur Gasphasenpolymerisation von Olefinen
US63108204P 2004-11-23 2004-11-23
PCT/EP2005/011935 WO2006050907A1 (fr) 2004-11-09 2005-11-08 Appareil et procédé pour la polymérisation d'oléfines en phase gazeuse

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Publication Number Publication Date
EP1831263A1 EP1831263A1 (fr) 2007-09-12
EP1831263B1 true EP1831263B1 (fr) 2008-12-10

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US (1) US7776278B2 (fr)
EP (1) EP1831263B1 (fr)
CN (1) CN101048429B (fr)
DE (1) DE102004054304A1 (fr)
WO (1) WO2006050907A1 (fr)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102004054628A1 (de) 2004-11-11 2006-05-18 Basell Polyolefine Gmbh Vorrichtung zur Gasphasenpolymerisation von Olefinen, insbesondere Ethylen
BRPI0821808A2 (pt) 2007-12-27 2015-06-16 Univation Tech Llc Sistemas e métodos para remover particulados carregados de fluxos de gás, e sistemas reatores que implementam os mesmos
CN112516949A (zh) * 2020-11-16 2021-03-19 南阳师范学院 具有产品分离功能的反应设备
CN112546992A (zh) * 2020-11-23 2021-03-26 山东无棣海丰电缆有限公司 一种节能环保交联反应装置

Family Cites Families (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3687920A (en) * 1971-01-25 1972-08-29 Union Carbide Corp Polymerization of olefins with silane modified catalyst system
US4486207A (en) * 1981-06-22 1984-12-04 Atlantic Richfield Company Apparatus for reducing attrition of particulate matter in a chemical conversion process
DZ520A1 (fr) 1982-03-24 2004-09-13 Union Carbide Corp Procédé perfectionné pour accroitre le rendement espace temps d'une réaction de polymérisation exothermique en lit fluidisé.
US4740550A (en) * 1986-06-18 1988-04-26 Shell Oil Company Multistage copolymerization process
US4764190A (en) * 1987-02-10 1988-08-16 Westinghouse Electric Corp. High temperature, high pressure gas filter system
FR2618786B1 (fr) * 1987-07-31 1989-12-01 Bp Chimie Sa Procede de polymerisation d'olefines en phase gazeuse dans un reacteur a lit fluidise
DE3930765C1 (en) 1989-09-14 1991-02-28 Metallgesellschaft Ag, 6000 Frankfurt, De Tubular gas filter - has several chambers contg. filter elements in housing, with dust collection bunker under each chamber
FR2666338B1 (fr) 1990-08-31 1994-04-08 Bp Chemicals Snc Procede regule de polymerisation d'olefine en phase gazeuse effectue a l'aide d'un catalyseur a base d'oxyde de chrome.
DE4217171A1 (de) 1992-05-23 1993-11-25 Basf Ag Kontinuierliches Gasphasenwirbelschichtverfahren zur Herstellung von Ethylenhomopolymerisaten und -copolymerisaten
US5521264A (en) * 1995-03-03 1996-05-28 Advanced Extraction Technologies, Inc. Gas phase olefin polymerization process with recovery of monomers from reactor vent gas by absorption
US5771844A (en) * 1996-04-04 1998-06-30 Foster Wheeler Development Corp. Cyclone separator having increased gas flow capacity
DE19728141A1 (de) * 1997-07-02 1999-01-07 Basf Ag Verfahren zur Polymerisation von C2-C8-Alk-1-enen mittels eines Ziegler-Natta-Katalysatorsystems
DE19754380A1 (de) * 1997-12-09 1999-06-10 Basf Ag Gasphasenwirbelschichtverfahren und danach erhältliche Ethylenhomo- und -copolymere
PT102166B (pt) 1998-06-08 2000-03-31 Romualdo Luis Ribera Salcedo Ciclones de elevada eficiencia
DE19915106A1 (de) * 1999-04-01 2000-10-05 Elenac Gmbh Verfahren zur Isolierung von Olefinen aus Polyolefinanlagen
DE10156202A1 (de) * 2001-11-15 2003-06-05 Basell Polyolefine Gmbh Kontinuierliches Gasphasenpolymerisationsverfahren
CN2526321Y (zh) * 2002-01-29 2002-12-18 宜宾天原集团有限公司 本体聚合反应产物后处理器
EP1487588B1 (fr) * 2002-03-19 2007-07-11 Ineos Europe Limited Separation de gaz et de solides au moyen d'un cyclone
AU2003226488A1 (en) 2002-03-19 2003-10-08 Bp Chemicals Limited Separation of gases and solids using a cyclone
DE102004054628A1 (de) 2004-11-11 2006-05-18 Basell Polyolefine Gmbh Vorrichtung zur Gasphasenpolymerisation von Olefinen, insbesondere Ethylen

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CN101048429B (zh) 2010-06-16
EP1831263A1 (fr) 2007-09-12
CN101048429A (zh) 2007-10-03
DE102004054304A1 (de) 2006-05-11
US20080014128A1 (en) 2008-01-17
US7776278B2 (en) 2010-08-17

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